WO2013093229A1

WO2013093229A1 - Catalyst usable in hydroconversion and including at least one zeolite and group viii and vib metals, and preparation of the catalyst

Info

Publication number: WO2013093229A1
Application number: PCT/FR2012/000488
Authority: WO
Inventors: Laurent Simon; Bertrand Guichard; Grégory LAPISARDI; Hughes Dulot; Valentina DE GRANDI; Delphine Minoux; Jean-Pierre Dath
Original assignee: IFP Energies Nouvelles; Total Raffinage Marketing
Priority date: 2011-12-22
Filing date: 2012-11-27
Publication date: 2013-06-27
Also published as: CN104321140B; FR2984760B1; BR112014015026A2; RU2014130021A; JP2015506828A; EP2794099B1; RU2621053C2; FR2984760A1; DK2794099T3; EP2794099A1; CO7121343A2; JP6302840B2; MX356504B; KR20140123938A; US9079174B2; ZA201404045B; MX2014007371A; CN104321140A; KR101853524B1; US20130180886A1

Abstract

The invention relates to a catalyst containing a support including at least one binder and at least one zeolite and having at least one series of channels, the opening of which is defined by a ring containing 12 oxygen atoms, said catalyst including phosphorus, at least one C1-C4 dialkyl succinate, acetic acid, and a hydro-dehydrogenating function that contains at least one Group VIB element and at least one Group VIII element. The Raman spectrum of said catalyst includes 990 and/or 974 cm^-1 bands characteristic of at least one Keggin heteropolyanion, bands characteristic of said succinate, and the main 896 cm^-1band characteristic of acetic acid. The invention also relates to the method for preparing the catalyst and to the use of said catalyst in hydroconversion.

Description

HYDROCONVERSION USING CATALYST COMPRISING AT LEAST ONE ZEOLITE AND METALS OF GROUP VIII AND VIB AND PREPARATION OF CATALYST

The invention relates to a catalyst comprising a zeolite, its process of preparation and a hydrocracking process using this catalyst.

PRIOR ART

The hydrocracking of heavy oil cuts is a very important refining process which makes it possible to produce lighter fractions, such as the gasolines, fuels and diesel fuel that the refiner seeks to adapt its production, from excessively heavy surpluses that can not be upgraded. to the structure of the request. This is a method widely described in the literature.

Hydrocracking is a process which derives its flexibility from three main elements which are the operating conditions used, the types of catalysts employed and the fact that the hydrocracking of hydrocarbon feeds can be carried out in one or two stages.

The hydrocracking catalysts used in the hydrocracking processes are all of the bifunctional type associating an acid function with a hydrogenating function. The acid function is provided by acidic supports whose surfaces generally vary from 150 to 800 m ² / g ^-1, such as halogenated aluminas (chlorinated or fluorinated in particular), the combinations of oxides of boron and aluminum, and more often amorphous silica-alumina and zeolites in combination with a generally aluminum binder. The hydrogenating function is provided either by one or more metals of group VIB of the periodic table of elements, or by a combination of at least one metal of group VIB of the periodic table and at least one metal of group VIII deposited on the support .

The bifunctionality of the catalyst, that is to say the ratio, the force and the distance between the acidic and hydrogenating functions is a key parameter known to those skilled in the art to influence the activity and the selectivity of the catalyst. A weak acid function and a strong hydrogenating function give low active catalysts, working at generally high temperature (greater than or equal to 390-400 ° C.), and at low feed-in space velocity (the VVH expressed in volume of charge at treat per unit volume of catalyst and per hour is generally less than or equal to 2), but with a very good selectivity in middle distillates (jet fuels and diesel fuels). Conversely, a strong acid function and a low hydrogenation function give active catalysts, but with lower selectivities in middle distillates.

Catalysts comprising zeolites have a good catalytic activity, but have selectivities in middle distillates (jet fuels and gas oils) often insufficient.

The prior art reports numerous works to improve the selectivity in middle distillates of zeolitic catalysts. The latter are composed of a hydrogenating phase of very variable composition (different metals), generally deposited on a support containing a zeolite, most often zeolite Y. The hydrogenating phase is active in sulphide form.

For example, mention may be made of the work relating to the dealumination by steaming or acid attack of zeolite Y, the modification of zeolite Y, the use of composite catalysts, or the use of small crystals of zeolites Y. Other patents as the WO2007126419 claim the use of zeolite mixture such as Beta and USY for improving the performance of hydrocracking catalysts.

Few studies on hydrocracking are devoted to the study of the nature and the modification of the metallic phase within the catalyst. One can quote the patent US5232578 which describes a process of hydrocracking in several catalytic beds with catalysts having different contents of metals, the patent application FR11 / 00.043 which claims the use of two distinct metal phases or the patent US6524470 which describes the addition of promoter.

For hydrotreatment reactions, the addition of an organic compound to monofunctional hydrotreatment catalysts to enhance their activity in HDS, HDA or HDA is now well known to those skilled in the art. Many patents protect the use of different ranges of organic compounds, such as mono, di or polyalcohols.

Patent WO11080407 proposes a process for the preparation and the use in the hydrotreatment processes of a catalyst comprising metals of groups VI B and VIII, an amorphous support based on alumina, phosphorus, a dialkyl succinate C1- C4 and a hydro-dehydrogenating function, a catalyst whose Raman spectrum comprises the the most intense bands characteristic of Keggin heteropolyanions (974 and / or 990 cm ^-1 ), C1-C4 dialkyl succinate and acetic acid (896 cm ^-1 ).

The present application provides a means for improving the middle distillate selectivity of zeolitic catalysts while maintaining or improving the catalytic activity.

DESCRIPTION OF THE INVENTION

The present invention relates to a catalyst containing a support comprising at least one binder and at least one zeolite having at least one series of channels whose opening is defined by a ring containing 12 oxygen atoms, said catalyst comprising phosphorus, at least a C1-C4 dialkyl succinate, acetic acid and a hydro-dehydrogenating function comprising at least one group VIB element and at least one group VIII element, whose Raman spectrum comprises the 990 and / or 974 bands; cm ¹ characteristics of at least one Keggin heteropolyanion, the characteristic bands of said succinate and the main band at 896 cm ^-1 characteristic of acetic acid.

The invention also relates to its preparation process which will be described later. This catalyst can be used for the hydroconversion (hydrocracking) of hydrocarbon feeds.

It makes it possible to obtain an improvement in the catalytic performances (in particular the iso-conversion middle distillate selectivity) with respect to the catalysts of the prior art. Indeed, it has been demonstrated that the use of the C1-C4 dialkyl succinate couple, and in particular dimethyl, and acetic acid on a dried catalyst precursor comprising one or a mixture of several zeolites and metals of groups VIB and VIII surprisingly leads to a significantly improved iso-conversion middle distillate selectivity compared to that obtained on the corresponding conventional catalysts. The implementation of the invention makes it possible to obtain a gain in activity but not at the expense of the selectivity for middle distillates. The catalyst obtained has a characteristic Raman spectrum comprising:

1) characteristic bands of the heteropolyanions of the Keggin PXYuGV and / or PY1 ₂ GV ^"type where Y is a Group VIB metal and X is a Group VIII metal According to Griboval, Blanchard, Payen, Fournier, Dubois in Catalysis Today 45 (1998) 277 Fig. 3 e), the main bands of structure PCoMon0 ₄ o ^" are on dried catalyst at 232, 366, 943, 974 cm ^-1 The most intense band characteristic of this type of HPA Keggin's gap is 974 cm ^-1 .1 According to Griboval, Blanchard, Gengembre, Payen, Fournier, Dubois, Bernard, Journal of Catalysis 188 (1999) 102, Fig. 1 (a), the principal bands of PMo ₁₂ 0 ₄ o ^{x "} are in the mass state of the HPA, for example with cobalt in counter ion at 251, 603, 902, 970, 990 cm ^'1 . The most intense band characteristic of this HPA Keggin is at 990 cm ^"1. MT Pope" heteropolys and isopoly oxometalates ", Springer Verlag, pp 8, also teaches that these bands are not natural characteristics of the atom X or Y, but of the structure of the Keggin HPA, complete, lacunary or substituted.

2) characteristic bands of the dialkyl succinate (s) used. The Raman spectrum of dimethyl succinate is an unambiguous imprint of this molecule.

In the spectral zone 300-1800 cm ^-1 , this spectrum is characterized by the following series of bands (only the most intense bands are reported, in cm ^'1 ): 391, 853 (most intense band), 924, 964 1739 cm ^-1 The spectrum of diethyl succinate has the following main bands in the spectral zone considered: 861 (most intense band), 1101, 1117 cm ^-1 . Similarly to dibutyl succinate: 843, 1123, 1303, 1439, 1463 ^cm ^-1 and diisopropyl succinate: 833, 876, 1149, 1185, 1469 (the most intense band), 1733 ^{cm -1.}

3) characteristic bands of acetic acid, the main ones: 448, 623, 896 cm ^-1 . The most intense band is 896 cm ^'1 . The exact position of the bands, their shapes and their relative intensities may vary to a certain extent depending on the recording conditions of the spectrum, while remaining characteristic of this molecule. Raman spectra of organic compounds are otherwise well documented in either the Raman spectrum databases (see, for example, Spectral Database for Organic Compounds, http: // riodb01j ^' base.aist.goj ^' p / sdbs / cgi-bin / clirect_frarne_top.cgi) or by the suppliers of the product (see for example, www.sigmaaldrich.com).

Raman spectra were obtained with a dispersive Raman-type spectrometer equipped with an argon ion laser (514 nm). The laser beam is focused on the sample using a microscope equipped with a x50 long-distance working lens. The laser power at the sample level is of the order of 1 mW. The Raman signal emitted by the sample is collected by the same objective and is dispersed using a 1800 rpm network and then collected by a CCD detector. The spectral resolution obtained is of the order of 0.5 cm ^-1 The recorded spectral zone is between 300 and 1800 cm ^-1 The acquisition duration was set at 120 s for each recorded Raman spectrum.

Preferably, the dialkyl succinate used is dimethyl succinate, and the catalyst has in its spectrum the main Raman bands at 990 and / or 974 cm ^-1 characteristic of the Keggin heteropolyanion (s), and 853 cm ^-1 characteristic of dimethyl succinate and 896 cm ^-1 characteristic of acetic acid. Preferably, the catalyst of the invention comprises a support formed of one or a mixture of zeolites (as defined in the invention, preferably zeolites of type Y and / or beta) and at least one binder which is preferably alumina and / or silica-alumina. Preferably, the support consists of alumina and zeolite. or silica-alumina and zeolite. The catalyst according to the invention may also comprise boron and / or fluorine and / or silicon.

There is also described a process for preparing the catalyst according to the invention, which comprises at least one step of impregnating a catalyzed precursor dried at a temperature below 80 ° C optionally containing phosphorus and a hydro-dehydrogenating function, as well as a support based on at least one zeolite formed in a binder, with an impregnating solution comprising the combination of acetic acid and C1-C4 dialkyl succinate and the phosphorus compound, if it does not has not been introduced in full previously, followed by a step of maturing said impregnated catalyst precursor, then a drying step at a temperature below 180 ° C, without step of subsequent calcination; the catalyst obtained is preferably subjected to a sulphurization step.

DETAILED DESCRIPTION

The preparation of a catalyst according to the invention comprises the following successive steps which will be detailed below: a) at least one step of impregnating a support, comprising at least one binder and at least one zeolite having at least a series of channels whose opening is defined by a ring containing 12 oxygen atoms, with at least one solution containing the elements of the hydro-dehydrogenating function, and phosphorus; the product obtained "catalytic precursor", b) drying at a temperature below 180 ° C without subsequent calcination, the product obtained "dried catalyst precursor", c) at least one impregnation step with a solution of impregnation comprising at least one C1-C4 dialkyl succinate, acetic acid and at least one phosphorus compound, if it has not been introduced completely in step a); the product obtained "impregnated dried catalyst precursor" will be referred to as "d) a maturing step, e) a drying step at a temperature below 180 ° C., without a subsequent calcination step; the product obtained will be called "catalyst".

Preferably, the product obtained at the end of step e) undergoes a f) sulphurization step.

As will be described later, the preparation of the catalyst according to the invention is preferably carried out with the following modes taken alone or in combination: the support is based on at least one zeolite formed in at least one binder; all of the hydrogenating function being introduced during step a); the dialkyl succinate is dimethyl succinate; step c) is carried out in the absence of solvent; step d) is carried out at a temperature of 17 to 50 ° C and step e) is carried out at a temperature between 80 and 160 ° C.

In a very preferred manner, the preparation of the catalyst according to the invention comprises the following successive stages: a) at least one step of dry impregnation of said support, based on at least one zeolite formed in a binder, with a solution containing all the elements of the hydro-dehydrogenating function, and phosphorus, b) drying at a temperature between 75 and 130 ° C without subsequent calcination, c) at least one step of dry impregnation with a solution of impregnation comprising dimethyl succinate and acetic acid, d) a maturation step at 17-50 ° C, e) a drying step at a temperature between 80 and 160 ° C, without subsequent calcination step.

The catalytic precursor containing the hydro-dehydrogenating function and the support based on at least one zeolite formed in at least one binder and its method of preparation are described below.

Said catalytic precursor obtained at the end of step a) of the process according to the invention can be prepared for the most part by all methods well known to those skilled in the art. Said catalytic precursor contains a hydro-dehydrogenating function and optionally contains phosphorus and / or boron and / or fluorine as a dopant, as well as the support based on at least one zeolite formed in a binder. The hydro-dehydrogenating function comprises at least one Group VIB element and at least one Group VIII element. Said catalytic precursor contains a support based on at least one zeolite shaped by advantageously using a porous binder, preferably amorphous, consisting of at least one refractory oxide. Said binder is advantageously chosen from the group formed by alumina, silica, clays, titanium oxide, boron oxide and zirconia, taken alone or as a mixture. The binder may consist of a mixture of at least two of the oxides mentioned above, and preferably silica-alumina. It is also possible to choose aluminates. It is preferred to use binders containing alumina, in all these forms known to those skilled in the art, for example gamma-alumina. The preferred binders are alumina and silica-alumina. Said catalytic precursor contains a support based on at least one zeolite which comprises at least one series of channels whose opening is defined by a ring containing 12 oxygen atoms (12MR). Said zeolite is advantageously chosen from zeolites defined in the "Atlas of Zeolite Framework Types" classification, 6th revised edition, Ch. Baerlocher, LB Me Cusker, DH Oison, 6th Edition, Elsevier, 2007, Elsevier "presenting at least one series of channels whose pore opening is defined by a ring containing 12 oxygen atoms.The zeolite initially used, before being modified, advantageously contains, in addition to at least one series of channels whose pore opening is defined by a ring containing 12 oxygen atoms (12MR), at least one series of channels whose pore opening is defined by a ring containing 8 oxygen atoms (8 MR) and / or at least one series of channels whose pore opening is defined by a ring containing 0 oxygen atoms (10 MR).

The zeolite contained in the support of said catalytic precursor may advantageously contain at least one other element T, different from silicon and aluminum, integrating in tetrahedral form into the framework of the zeolite. Preferably, said element T is chosen from iron, germanium, boron and titanium and represents a portion by weight of between 2 and 30% of all the constituent atoms of the zeolitic framework other than the oxygen atoms. The zeolite then has an atomic ratio (Si + T) / Al of between 2 and 200, preferably of between 3 and 100 and very preferably of between 4 and 80, T being defined as above.

Preferably, the zeolite initially used is chosen from the group FAU, BEA, ISV, IWR, IWW, MEI, UWY and very preferably, the initial zeolite is taken from the FAU and BEA group. Preferably it is a zeolite of FAU and / or BEA type, such as zeolite Y and / or beta.

The zeolite used according to the invention may have undergone treatments in order to stabilize it or to create mesoporosity. These modifications are carried out by at least one of the dealumination techniques known to those skilled in the art, for example hydrothermal treatment or acid attack. Preferably, this modification is carried out by combining three types of operations known to those skilled in the art: hydrothermal treatment, ion exchange and acid attack. The said zeolite can also undergo so-called disilication treatments. by basic solutions, and we can cite more specifically without restricting treatments with NaOH or Na ₂ CO ₃ combined or not with a dealumination treatment.

The zeolite modified or not used in the support may be, without limitation, for example in the form of powder, ground powder, suspension, suspension having undergone a deagglomeration treatment. Thus, for example, the zeolite can advantageously be slurried acidulated or not at a concentration adjusted to the final zeolite content referred to the support. This suspension commonly called a slip is then advantageously mixed with the precursors of the matrix.

According to a preferred method of preparation, the zeolite can advantageously be introduced during the shaping of the support with the elements that constitute the matrix. For example, according to this preferred embodiment of the present invention, the zeolite according to the invention is added to a wet alumina gel during the step of forming the support.

According to another preferred method of preparation, the zeolite can be introduced during the synthesis of the matrix. For example, according to this preferred embodiment of the present invention, the zeolite is added during the synthesis of the silicoaluminum matrix; the zeolite may be added to a mixture of an acidic alumina compound with a fully soluble silica compound.

The support can be shaped by any technique known to those skilled in the art. The shaping can be carried out for example by extrusion, pelletizing, by the method of coagulation in drop (oil-drop), by rotating plate granulation or by any other method well known to those skilled in the art. The catalysts used in the process according to the invention advantageously have the form of spheres or extrudates. It is however advantageous that the catalyst is in the form of extrudates with a diameter of between 0.5 and 5 mm and more particularly between 0.7 and 2.5 mm. The shapes are cylindrical (which can be hollow or not), cylindrical twisted, multilobed (2, 3, 4 or 5 lobes for example), rings. The trilobal form is preferably used, but any other form can be used. The catalysts according to the invention may optionally be manufactured and used in the form of crushed powder, tablets, rings, balls, wheels.

The hydro-dehydrogenating function of said catalytic precursor is provided by at least one group VIB element and at least one Group VIII element. The total content of hydro-dehydrogenating elements is advantageously greater than 6% by weight oxide based on the total weight of the catalyst. The preferred group VIB elements are molybdenum and tungsten. The preferred group VIII elements are non-noble elements and in particular cobalt and nickel. Advantageously, the hydrogenating function is chosen from the group formed by the combinations of nickel-molybdenum or nickel-cobalt-molybdenum or nickel-molybdenum-tungsten elements.

The molybdenum precursors that can be used are also well known to those skilled in the art. Reference is made to the patent application WO-2011/080407 which describes these precursors as well as those of tungsten, and more generally those of the elements of groups VIII and VIB.

The amounts of the precursors of the group VIB elements are advantageously between 5 and 40% by weight of oxides relative to the total mass of the catalytic precursor, preferably between 8 and 37% by weight and very preferably between 10 and 35% by weight. .

The amount of the precursors of the group VIII elements is advantageously between 1 and 10% by weight of oxides relative to the total mass of the catalytic precursor, preferably between 1.5 and 9% by weight and very preferably between 2 and 8% weight The hydro-dehydrogenating function of said catalytic precursor can advantageously be introduced into the catalyst at various levels of the preparation and in various ways. Said hydro-dehydrogenating function can advantageously be introduced in part during the shaping of said amorphous support or preferably after this shaping. Advantageously, all of the hydro-dehydrogenating function is introduced during step a).

In the case where the hydro-dehydrogenating function is introduced in part during the shaping of said amorphous support, it can be introduced in part (for example at most 10% of element (s) of group VIB is introduced by mixing) only at the moment of mixing with an alumina gel chosen as a matrix, the remainder of the hydrogenating element (s) being then introduced later. Preferably, when the hydro-dehydrogenating function is introduced in part at the time of kneading, the proportion of group VIB element introduced during this step is less than 5% of the total amount of group VIB element introduced on the the final catalyst. Preferably, the group VIB element is introduced at the same time as the group VIII element, regardless of the mode of introduction.

In the case where the hydro-dehydrogenating function is introduced at least partly and preferably completely, after the shaping of said amorphous support, the introduction of said hydro-dehydrogenating function on the amorphous support can be advantageously carried out by one or several impregnations in excess of solution on the shaped and calcined support, or preferably by one or more dry impregnations and, preferably, by dry impregnation of said shaped and calcined support, using solutions containing the precursor salts of metals. Very preferably, the hydro-dehydrogenating function is introduced in full after shaping of said amorphous support, by dry impregnation of said support with an impregnating solution containing the precursor salts of the metals. The introduction of said hydro-dehydrogenating function can also be advantageously carried out by one or more impregnations of the shaped and calcined support by a solution of the precursor (s) of the active phase. In the case where the elements are introduced in several impregnations of the corresponding precursor salts, an intermediate drying step of the catalyst is generally carried out at a temperature of between 50 and 180 ° C., preferably between 60 and 150 ° C. and very preferably between 75 and 130 ° C. Phosphorus is also introduced into the catalyst. Another dopant of the catalyst may also be introduced which is selected from boron, fluorine alone or as a mixture. The dopant is an added element, which in itself has no catalytic character but which increases the catalytic activity of the metal (metals). Said dopant may advantageously be introduced alone or as a mixture with at least one of the elements of the hydro-dehydrogenating function. It can also be introduced as soon as the support is synthesized. It can also be introduced just before or just after peptization of the chosen matrix, such as, for example, and preferably aluminum oxyhydroxide (boehmite) precursor of alumina. Said dopant may also advantageously be introduced in admixture with the precursor (s) of the hydro-dehydrogenating function, in whole or in part on the shaped amorphous support, preferably alumina or silica-alumina in the form of extruded, by dry impregnation of said amorphous support with a solution containing the metal precursor salts and the precursor (s) of the dopant (s). Finally, the dopant, in particular when this is phosphorus, may be introduced with the dialkyl succinate.

The sources of boron and fluorine are also described in application WO-2011/30807

The preferred phosphorus source is orthophosphoric acid H ₃ PO ₄ , but its salts and esters as ammonium phosphates are also suitable. Phosphorus may also be introduced together with the group VIB element (s) as Keggin, Keggin lacunary, Keggin substituted or Strandberg heteropolyanions.

The dopant is advantageously introduced into the catalytic precursor in an amount of oxide of said dopant relative to the catalyst:

between 0 and 40%, preferably between 0 and 30% and even more preferably between 0 and 20%, preferably between 0 and 15% and even more preferably between 0 and 10% when said dopant is boron; when boron is present, preferably the minimum amount is 0.1% by weight,

between 0.1 to 20%, preferably between 0.1 and 15% and even more preferably between 0.1 and 10% by weight, when said dopant is phosphorus, - between 0 and 20%, preferably between 0 and 15% and even more preferably between 0 and 10%, when said dopant is fluorine; when fluorine is present, preferably the minimum amount is 0.1% by weight.

Phosphorus is always present. It is introduced at least by impregnation on the catalytic precursor during step a) and / or on the catalytic precursor dried in step c). Preferably, it is the same for the other dopants. However, as mentioned above, the dopants can be introduced in part during the preparation of the support (shaping included) or in whole (with the exception of phosphorus). The introduction of said hydro-dehydrogenating function and optionally a dopant in or on the calcined support formed is then advantageously followed by a drying step b) during which the solvent of the precursor metal salts of (or ) (metal oxide) (solvent which is usually water) is removed at a temperature between 50 and 180 ° C, preferably between 60 and 150 ° C or between 65 and 150 ° C and very preferably between 70 and 140 ° C or between 75 and 130 ° C. The drying step of the "dried catalyst precursor" thus obtained is never followed by a calcination step in air, for example at a temperature above 200 ° C.

Preferably, in step a) of the process according to the invention, said "catalytic precursor" is obtained by dry impregnation of a solution comprising a precursor (s) of the hydro-dehydrogenating function, and the phosphorus on a calcined support based on at least one zeolite shaped in a shaped binder, followed by drying at a temperature below 180 ° C, preferably between 50 and 180 ° C, preferably between 60 and 150 ° C and very preferably between 75 and 130 ° C.

It is thus obtained is a "dried catalyst precursor" at the end of step b).

It is possible in step a) of the process according to the invention to prepare an impregnating solution containing at least one dopant chosen from boron, fluorine, taken alone or as a mixture Even more preferably, the "catalytic precursor" in step a) of the process according to the invention is prepared with an impregnating solution containing at least one precursor of each element of the hydro-dehydrogenating function, in the presence of a phosphorus precursor, the support based on at least one zeolite formed in a binder consisting of alumina or silica-alumina.

According to step c) of the process according to the invention, said dried catalyst precursor is impregnated with an impregnation solution comprising at least one C1-C4 dialkyl succinate (and in particular dimethyl succinate) and the acid acetic.

Said compounds are advantageously introduced into the impregnating solution of stage c) of the process according to the invention in a corresponding amount:

1) at a molar ratio of dialkyl succinate (for example dimethyl) per element (s) of the GVIB group impregnated with the catalytic precursor of between 0.15 to 2.5 mol / mol, preferably between 0.3 and 2, 0 mole / mole, preferably between 0.5 and 1.8 mole / mole and very preferably between 0.8 and 1.6 mole / mole, and

2) at a molar ratio of acetic acid per element (s) of the GVIB group impregnated with the catalytic precursor of between 0.1 and 0 mol / mol, preferably between 0.5 and 8 mol / mol, and preferably between between 1, 3 and 7.5 mole / mole and very preferably between 1, 5 and 7 mole / mole. According to step c) of the process according to the invention, the combination of dialkyl succinate and acetic acid is introduced onto the dried catalyst precursor by at least one impregnation step and preferably by a single impregnation step of a impregnating solution on said dried catalyst precursor.

Said combination may advantageously be deposited in one or more steps either by slurry impregnation, or by excess impregnation, or by dry impregnation, or by any other means known to those skilled in the art.

According to a preferred embodiment of step c) of the preparation process according to the invention, step c) is a single step of dry impregnation. According to step c) of the process according to the invention, the impregnating solution of step c) comprises at least the combination of C1-C4 dialkyl succinate (in particular dimethyl) and acetic acid.

The impregnating solution used in stage c) of the process according to the invention can be completed by any non-protic solvent known to those skilled in the art including toluene, xylene.

The impregnation solution used in stage c) of the process according to the invention can be completed by any polar solvent known to those skilled in the art. Said polar solvent used is advantageously chosen from the group formed by methanol, ethanol, water, phenol and cyclohexanol, taken alone or as a mixture. Said polar solvent used in stage c) of the process according to the invention may also be advantageously chosen from the group formed by propylene carbonate, DMSO (dimethylsulfoxide) or sulfolane, taken alone or as a mixture. Preferably, a polar protic solvent is used. A list of the usual polar solvents and their dielectric constant can be found in the book Solvents and Solvent Effects in Organic Chemistry, C. Reichardt, Wiley-VCH, 3rd Edition, 2003, pp. 472-474. the solvent that may be used is ethanol.

Preferably, there is no solvent in the impregnating solution used in step c) of the process according to the invention, which facilitates the implementation on an industrial scale. Preferably, it contains only dialkyl succinate and acetic acid.

The dialkyl succinate used is preferably included in the group consisting of dimethyl succinate, diethyl succinate, dipropyl succinate, diisopropyl succinate and dibutyl succinate. Preferably, the C1-C4 dialkyl succinate used is dimethyl succinate or diethyl succinate. At least one C1-C4 dialkyl succinate is used. Very preferably, the C1-C4 dialkyl succinate used is dimethyl succinate, preferably alone.

According to step d) of the preparation process according to the invention, the dried impregnated catalytic precursor from step c) is subjected to a maturation step. It is advantageously carried out at atmospheric pressure and at a temperature of between 17 ° C and 50 ° C and generally a maturation period of between ten minutes and forty eight hours and preferably between thirty minutes and five hours, is sufficient. Longer durations are not excluded. A simple way to adjust the maturation time is to characterize the formation of Keggin heteropolyanions by Raman spectroscopy in the impregnated dried catalyst precursor from step c) of the process according to the invention. In a very preferred manner, to increase the productivity without modifying the amount of reformed heteropolyanions, the duration of the maturation is between thirty minutes and four hours. Even more preferably, the duration of the maturation is between thirty minutes and three hours. According to step e) of the preparation process according to the invention, the matured impregnated dried catalyst precursor from step d) is subjected to a drying step at a temperature below 180 ° C., without a subsequent calcination step. for example a temperature above 200 ° C.

The purpose of this step is to obtain a transportable, storable, and manipulable catalyst, in particular for the loading of the hydrotreatment unit. It is advantageous, according to the embodiment of the invention chosen, to remove all or part of the possible solvent that has allowed the introduction of the combination of C1-C4 dialkyl succinate (in particular dimethyl) and acetic acid. In all cases, and especially in the case where the combination of C1-C4 dialkyl succinate (in particular dimethyl) and acetic acid is used alone, it is a question of giving a dry aspect to the catalyst, in order to avoid that the extrusions do not stick to each other during the transport, storage, handling or loading steps.

The drying step e) of the process according to the invention is advantageously carried out by any technique known to those skilled in the art. It is advantageously carried out at atmospheric pressure or under reduced pressure. This step is preferably carried out at atmospheric pressure.

This step e) is advantageously carried out at a temperature above 50 ° C and below 180 ° C, preferably between 60 and 170 ° C and very preferably between 80 and 160 ° C. It is advantageously carried out in crossed bed using air or any other hot gas. Preferably, when the drying is carried out in a fixed bed, the gas used is either air or an inert gas such as argon or nitrogen. In a very preferred manner, the drying is carried out in a bed traversed in the presence of nitrogen. Preferably, this step has a duration of between 15 minutes and 4 hours and preferably between 30 minutes and 3 hours and very preferably between 1 hour and 3 hours.

At the end of step e) of the process according to the invention, a dried catalyst is obtained which is not subjected to any subsequent calcination step in air, for example at a temperature above 200 ° C.

The catalyst obtained after step d) or step e) has a Raman spectrum comprising the most intense bands at 990.974 cm ^-1 (Keggin type heteropolyanions), the bands corresponding to the succinate ( for dimethyl succinate the most intense band is at 853 cm ^-1 , and the characteristic bands of acetic acid, the most intense at 896 cm ^-1 .

Prior to its use, it is advantageous to convert a dried or calcined catalyst to a sulphurized catalyst to form its active species. This activation or sulphurization phase is carried out by methods well known to those skilled in the art, and advantageously under a sulpho-reducing atmosphere in the presence of hydrogen and hydrogen sulphide.

At the end of step e) of the process according to the invention, said dried catalyst obtained is therefore advantageously subjected to a f) sulphurization step, without intermediate calcination step.

Said dried catalyst is advantageously sulphurized ex situ or in situ. The sulfurizing agents are H ₂ S gas or any other sulfur-containing compound used to activate hydrocarbon feeds to sulphurize the catalyst. Said sulfur-containing compounds are advantageously chosen from alkylsulfides such as, for example, dimethyl disulphide (DMDS), alkylsulphides, such as, for example, sulphide. of dimethyl, n-butyl mercaptan, polysulfide compounds tertiononylpolysulfide type such as for example the TPS-37 or TPS-54 marketed by Arkema, or any other compound known to those skilled in the art to obtain a good sulphurization of the catalyst. Preferably the catalyst is sulfided in situ in the presence of a sulfurizing agent and a hydrocarbon feedstock. Very preferably, the catalyst is sulphurized in situ in the presence of a hydrocarbon feed additive of dimethyl disulfide.

HYDROCONVERSION PROCESS

The invention relates to a process for hydroconversion of hydrocarbon feeds in the presence of the catalyst of the invention.

The hydroconversion process (hydrocracking) operates in the presence of hydrogen, generally at a temperature above 200 ° C, at a pressure greater than 1 MPa, the space velocity being between 0.1 and 20 h -1 and the amount hydrogen introduced is such that the ratio by volume liter of hydrogen / liter of hydrocarbon is between 80 and 5000 UL.

Preferably, the hydrocracking process is carried out in the presence of hydrogen at a temperature above 200 ° C., preferably between 250 and 480 ° C., preferably between 320 and 450 ° C., very preferably between 330 ° C. and 450 ° C. and 435 ° C., under a pressure greater than 1 MPa, preferably between 2 and 25 MPa, preferably between 3 and 20 MPa, at a space velocity of between 0.1 and 20 h -1, preferably 0.1 and 6 h -1, preferably between 0.2 and 3 h -1, and the amount of hydrogen introduced is such that the volume ratio of hydrogen liter / liter of hydrocarbon is between 80 and 5000 UL and the more often between 100 and 3000 UL.

These operating conditions used in these processes generally make it possible to achieve pass conversions, products having boiling points below 300 ° C., and better still below 340 ° C., and even more preferably below 370 ° C. at least 50% by weight and even more preferably between 20 and 100% but most typically between 60-95% by weight.

loads A wide variety of fillers can be processed by the processes according to the invention described above. They advantageously contain at least 20% by volume and preferably at least 80% by volume of compounds boiling above 340 ° C.

The filler is advantageously chosen from LCOs (Light Cycle Oil = light gas oils from a catalytic cracking unit), atmospheric distillates, vacuum distillates such as for example obtained from the direct distillation of the crude or from conversion units. such as FCC, coker or visbreaking, feeds from aromatics extraction units of lubricating oil bases or from solvent dewaxing of lubricating oil bases, distillates from desulphurization processes or hydroconversion in fixed bed, in bubbling bed or in slurry of RAT (atmospheric residues) and / or RSV (vacuum residues) and / or deasphalted oils, and deasphalted oils, taken alone or as a mixture. The list above is not exhaustive. Paraffins from the Fischer-Tropsch process are excluded. Said fillers preferably have a boiling point T5 greater than 340 ° C., preferably greater than 370 ° C., that is to say that 95% of the compounds present in the feed have a boiling point greater than 340 ° C. and preferably greater than 370 ° C.

The nitrogen content of the feedstocks treated in the processes according to the invention is advantageously greater than 500 ppm by weight, preferably between 500 and 10,000 ppm by weight, more preferably between 700 and 5000 ppm by weight and even more preferably between 1000 and 5000 ppm by weight. and 4000 ppm weight. The sulfur content of the fillers treated in the processes according to the invention is advantageously between 0.01 and 5% by weight, preferably between 0.2 and 4% by weight and even more preferably between 0.5 and 3%. % weight

The charge may optionally contain metals. The cumulative nickel and vanadium content of the fillers treated in the processes according to the invention is preferably less than 10 ppm by weight, preferably less than 5 ppm by weight and even more preferably 1 ppm by weight.

The charge may optionally contain asphaltenes. The asphaltene content is generally less than 3000 ppm by weight, preferably less than 1000 ppm by weight, more preferably less than 200 ppm by weight. Cribs

In the case where the feedstock contains resins and / or asphaltenes and / or metal type compounds, it is advantageous to first pass the feedstock over a bed of catalyst or adsorbent other than the hydrocracking or hydrotreatment catalyst. . The catalysts or guard beds used according to the invention are in the form of spheres or extrudates. It is however advantageous that the catalyst is in the form of extrudates with a diameter of between 0.5 and 5 mm and more particularly between 0.7 and 2.5 mm. The shapes are cylindrical (which can be hollow or not), cylindrical twisted, multilobed (2, 3, 4 or 5 lobes for example), rings. The cylindrical shape is preferably used, but any other shape may be used.

In order to remedy the presence of contaminants and / or poisons in the feed, the guard catalysts may, in another preferred embodiment, have more particular geometric shapes in order to increase their void fraction. The void fraction of these catalysts is between 0.2 and 0.75. Their outer diameter can vary between 1 and 35 mm. Among the particular forms possible without this list being exhaustive, we cite: hollow cylinders, hollow rings, Raschig rings, serrated hollow cylinders, crenellated hollow cylinders, pentaring carts, multi-hole cylinders, etc ..

These catalysts or guard beds may have been impregnated with an active phase or not. Preferably, the catalysts are impregnated with a hydro-dehydrogenation phase. Very preferably, the CoMo, NiMo or NiCoMo phases are used.

These catalysts or guard beds may have macroporosity. The guard beds can be marketed by Norton-Saint-Gobain, for example the MacroTrap® guard beds. Guard beds can be marketed by Axens in the ACT family: ACT077, ACT645, ACT961 or HMC841, HMC845, HMC868, HF858, HM848 or HMC945. It may be particularly advantageous to superpose these catalysts in at least two different beds of varying heights. The catalysts having the highest void content are preferably used in the first catalytic bed or first catalytic reactor inlet. It can also be advantageous to use at least two different reactors for these catalysts. Finally, it can also be made use of permutable guard beds to be able to handle the loads containing the most asphaltenes and metals.

Modes of realization

The hydrocracking processes according to the invention may advantageously employ said catalyst described above alone, in one or more fixed bed catalytic beds, in one or more reactors, in a so-called one-step hydrocracking scheme, with or without liquid recycling of the unconverted fraction, optionally in combination with a conventional hydrotreating catalyst located upstream of the catalyst used in the process according to the present invention. The hydrocracking processes according to the invention may advantageously also use said catalyst described above alone, in one or more bubbling bed reactors, in a so-called one-step hydrocracking scheme, with or without liquid recycling of the reactor. unconverted fraction, optionally in combination with a conventional hydrotreating catalyst located in a fixed bed or bubbling bed reactor upstream of the catalyst used in the process according to the present invention.

One-step process

The hydrocracking process according to the invention can advantageously be carried out in a so-called one-step process. The so-called hydrocracking in one step, comprises in the first place and in a general manner advanced hydrorefining which aims to perform a hydrodenitrogenation and desulphurization of the charge before it is sent to the hydrocracking catalyst itself , especially in the case where it comprises a zeolite. This extensive hydrorefining of the feed causes only a limited conversion of the feedstock into lighter fractions, which remains insufficient and must therefore be completed on the more active hydrocracking catalyst described above. However, it should be noted that no separation occurs between the two types of catalysts. The entire effluent at the outlet of the reactor is injected onto the hydrocracking catalyst proper and this is then that a separation of the formed products is achieved. This version of the hydrocracking, also called "Once Through", has a variant that has a recycling of the unconverted fraction to the reactor for further conversion of the charge. The catalyst described according to the invention is therefore advantageously used in a so-called hydrocracking process in a step, in a hydrocracking zone placed downstream of a hydrorefining zone, no intermediate separation being implemented. between the two areas.

Preferably, the hydrorefining catalyst used in the first hydrorefining reaction zone, alone or in combination with another conventional hydrorefining catalyst, located upstream of the catalyst described according to the invention, is a catalyst optionally comprising a doping element. selected from phosphorus, boron and silicon, said catalyst being based on non-noble group VIII elements and optionally in combination with group VIB elements on alumina or silica alumina support.

One-step process in fixed bed with intermediate separation

The hydrocracking process according to the invention can advantageously be implemented in a so-called fixed-bed process with intermediate separation.

Said method advantageously comprises a hydrorefining zone, an area allowing partial removal of the ammonia, for example by a hot flash, and a zone comprising said hydrocracking catalyst according to the invention. This process for the hydrocracking of hydrocarbon feeds in one step for the production of middle distillates and optionally of oil bases advantageously comprises at least a first hydrorefining reaction zone, and at least a second reaction zone, in which the hydrocracking is carried out. at least a portion of the effluent from the first reaction zone. This process also advantageously comprises an incomplete separation of the ammonia from the effluent leaving the first zone. This separation is advantageously carried out by means of an intermediate hot flash. The hydrocracking performed in the second reaction zone is advantageously carried out in the presence of ammonia in an amount less than the amount present in the feedstock. preferably less than 1500 ppm by weight, more preferably less than 1000 ppm by weight and even more preferably less than 800 ppm by weight of nitrogen.

The catalyst described according to the invention is therefore advantageously used in a hydrocracking process called a fixed-bed intermediate separation step, in a hydrocracking zone placed downstream from a hydrorefining zone, an intermediate separation. partial elimination of the ammonia being implemented between the two zones.

Preferably, the hydrorefining catalyst used in the first hydrorefining reaction zone, alone or in combination with another conventional hydrorefining catalyst, located upstream of the catalyst described according to the invention, is a catalyst optionally comprising a doping element. selected from phosphorus, boron and silicon, said catalyst being based on non-noble group VIII elements and optionally in combination with group VI B elements on alumina or silica support. Two-step process

The hydrocracking process according to the invention can advantageously be implemented in a so-called two-step process whose goal is maximum or even total conversion.

The two-stage hydrocracking comprises a first step whose objective, as in the "one-step" process, is to perform the hydrorefining of the feed, but also to achieve a conversion in the first step of the feed order. general from 40 to 60%. The effluent from the first step then undergoes separation (distillation), which is often called intermediate separation, which aims to separate the conversion products from the unconverted fraction. In the second step of a two-stage hydrocracking process, only the fraction of the unconverted feedstock in the first step is processed. This separation allows a two-stage hydrocracking process to be more selective in middle distillates (kerosene + diesel) than a one-step process. Indeed, the intermediate separation of the conversion products avoids their "over cracking" in naphtha and gas in the second step on the hydrocracking catalyst. Moreover, it should be noted that the unconverted fraction of the feedstock treated in the second Step generally contains very low levels of NH3 as well as organic nitrogen compounds, generally less than 20 ppm by weight or even less than 10 ppm by weight.

The catalyst bed configurations described in the case of a so-called one-step process can advantageously be used in the first step of a so-called two-step scheme, whether the catalyst according to the invention is used alone or in combination with a catalyst. conventional hydrorefining.

The catalyst described according to the invention is therefore advantageously used in a so-called two-stage hydrocracking process in the second hydrocracking stage placed downstream of the first hydrorefining step, an intermediate separation being carried out between both areas.

For the so-called one-step processes and for the first hydrorefining stage of two-stage hydrocracking processes, the conventional hydrorefining catalysts that may advantageously be used are the catalysts optionally comprising a doping element chosen from phosphorus, boron and silicon, said catalyst being based on non-noble group VIII elements and optionally in combination with group VIB elements on alumina or silica alumina support.

The examples which follow demonstrate the gains in activity and selectivity for large middle distillates on the catalysts prepared according to the process according to the invention compared to the catalysts of the prior art and specify the invention without, however, limiting its scope.

EXAMPLES

Example 1 Preparation of catalysts 1A (not in accordance with the invention) and 1B (in accordance with the invention)

Zeolite USY-1 (ultra-stable Y), the characteristics of which are described in Table 1, was used in the preparation of catalysts 1A and 1B. Table 1: Characteristic of the zeolite USY-1.

A matrix composed of ultrafine tabular boehmite or alumina gel, sold under the name SB3 by Condea Chemie GmbH was used. The support is obtained after shaping and extrusion by mixing 20% by weight of the zeolite USY-1 with 80% of alumina gel. The support is then calcined at 500 ° C. for 2 hours in air.

A solution composed of molybdenum oxide, nickel hydroxycarbonate and phosphoric acid is added to the support by dry impregnation to obtain a formulation of 3.1 / 18.0 / 3.1 expressed in% by weight of oxides relative to the amount of dry matter of the final catalyst. After dry impregnation, the extrudates are allowed to mature in a saturated water atmosphere for 12 hours and then dried overnight at 90 ° C. This catalytic precursor is called 1 PC. The catalytic precursor 1PC is finally calcined at 450 ° C. for 2 hours, resulting in calcined catalyst 1A (not in accordance with the invention). Catalyst 1B, according to the invention, is prepared by dry impregnation of the catalyst precursor PC with a solution comprising dimethyl succinate and acetic acid diluted in water. The target contents of dimethyl succinate (DMSU) and acetic acid (AA) are respectively 27% by weight and 18% by weight (ie AA / Mo = 2.7 mol / mol and DMSU / Mo = 1.5 mol / mol ). After a maturation period of 3 hours in a closed vessel at room temperature, the catalyst is once again dried under a stream of nitrogen (1 NUg / g) for 1 hour in a bed passed through at 140 ° C.

The Raman spectrum of catalyst 1B, according to the invention, is given on the. The most intense bands characteristic of dimethyl succinate at 391, 853, 924 and 964 cm- ¹ are clearly identifiable In the same way, the most intense band characteristic of acetic acid at 896 cm ^-1 is clearly visible. Finally, the bands The more intense characteristics of Keggin heteropolyanions at 251, 603 and 990 cm ^-1 are also clearly identifiable.

EXAMPLE 2 Preparation of catalysts 2A (not in accordance with the invention) and 2B (in accordance with the invention)

The zeolite USY-2 (ultra-stable Y) whose characteristics are described in Table 2 was used for the preparation of catalysts 2A (not in accordance with the invention) and 2B

(according to the invention).

Table 2: Characteristic of the zeolite USY-2.

A matrix composed of ultrafine tabular bcehmite or alumina gel, marketed under the name SB3 by Condea Chemie GmbH was used. The support is obtained after shaping and extrusion by mixing 20% by weight of the zeolite USY with 80% of alumina gel. The support is then calcined at 500 ° C. for 2 hours in air.

A solution composed of molybdenum oxide, nickel hydroxycarbonate and phosphoric acid is added to the support by dry impregnation to obtain a formulation of 3.1 / 18.0 / 3.1 expressed in% by weight of oxides relative to the amount of dry matter of the final catalyst. After dry impregnation, the extrudates are allowed to mature in a saturated water atmosphere for 12 hours and then dried overnight at 90 ° C. This catalytic precursor is called 2PC. The catalytic precursor 2PC is finally calcined at 450 ° C. for 2 hours, resulting in calcined catalyst 2A (not in accordance with the invention).

Catalyst 2B, according to the invention, is prepared by dry impregnation of the catalytic precursor 2PC with a solution comprising dimethyl succinate and acetic acid diluted in water. The target contents of dimethyl succinate (DMSU) and acetic acid (AA) are respectively 27% by weight and 18% by weight (ie AA / Mo = 2.7 mo / mol and DMSU / o = 1.5 mol / mol). After a maturation period of 3 hours in a closed vessel at room temperature, the catalyst is once again dried under nitrogen flow (1 NLJg / g) for 1 hour in a bed passed through at 140 ° C.

The Raman spectrum of catalyst 2B, according to the invention, comprises, as in the case of the Raman spectrum of catalyst B, the most intense bands characteristic of dimethyl succinate at 391, 853, 924 and 964 cm ^-1 , the band more intense characteristic of acetic acid at 896 cm ^-1 and finally, the most intense bands characteristics of Keggin type heteropolyanions at 251, 603 and 990 cm ^-1 .

Example 3 Preparation of catalysts 3A (not in accordance with the invention) and 3B (in accordance with the invention)

The zeolite USY-2 (ultra-stable Y) whose characteristics are described in Table 2 and the zeolite BETA whose characteristics are described in Table 3 were used to prepare the catalysts 3A (not in accordance with the invention) and 3B (according to the invention).

Table 3: Characteristic of BETA zeolite.

Catalyst 3 was prepared following the same procedure as that used in Examples 1 and 2 with the exception of the mixture of alumina gel and zeolite which is composed of 80% by weight of alumina gel with 17% by weight of zeolite USY-2 and 3% by weight of zeolite BETA. The impregnation solution used is equivalent with a final NiMoP content of respectively 3.1 / 18 / 3.1. As in Examples 1 and 2, the catalytic precursor 3PC is obtained after maturation and drying and calcined catalyst 3A (non-compliant) after calcination.

Catalyst 3B, according to the invention, is prepared by dry impregnation of the catalytic precursor 3PC with a solution comprising dimethyl succinate and acetic acid diluted in water. The target contents of dimethyl succinate (DMSU) and acetic acid (AA) are respectively 27% by weight and 18% by weight (ie AA / Mo = 2.7 mol / mol and DMSU / Mo = 1.5 mol / mol ). After a maturation period of 3 hours in a vacuum at room temperature, the catalyst is once again dried under nitrogen flow (1 NL / g / g) for 1 hour in a bed passed through at 140 ° C.

The Raman spectrum of catalyst 3B, according to the invention, comprises, as in the case of the Raman spectrum of catalysts 1B and 2B, the most intense bands characteristic of dimethyl succinate at 391, 853, 924 and 964 cm ^-1 , the most intense band characteristic of acetic acid at 896 cm ^-1, and finally the most intense bands characteristic of Keggin heteropolyanions at 251, 603 and 990 cm ^-1 .

Example 4: Evaluation of hydrocracking catalysts said a step of a vacuum distillate.

The catalysts whose preparations are described in the preceding examples are used under the conditions of high conversion hydrocracking (60-100%). The petroleum feed is a vacuum distillate having undergone a first hydrorefining stage on a catalyst whose main characteristics are given in Table 4.

No intermediate separation step is carried out between the prior hydrorefining step and the hydrocracking step.

Table 4: Characteristic of the load used.

Density (20/4) 0.869

Sulfur (ppm by weight) 502

Nitrogen (ppm weight) Simulated distillation initial point 298 ° C point 10% 369 ° C point 50% 427 ° C point 90% 481 ° C end point 538 ° C

0.6% by weight of aniline and 2% by weight of dimethyl disulfide are added to the feed in order to simulate the partial pressures of H ₂ S and of NH ₃ present in the second hydrocracking step. The feed thus prepared is injected into the hydrocracking test unit which comprises a fixed-bed reactor with up-flow of the feed ("up-flow"), into which 80 ml of catalyst is introduced. The catalyst is sulfided with an n-hexane / DMDS + aniline mixture up to 320 ° C. It should be noted that any in situ or ex situ sulphurization method is suitable. Once the sulfurization is complete, the charge described in Table 4 can be transformed. The operating conditions of the test unit are given in Table 5. Table 5: Catalysts test conditions.

Total pressure 9 Mpa

3

Catalyst 80 cm

Hydrogen flow 80 L / h

3

Charging rate 80 cm / h

The catalytic performances are expressed by the temperature which makes it possible to reach a gross conversion level of 70% and by the average distillates (DM) yields. These catalytic performances are measured on the catalyst after a period of stabilization, generally at least 48 hours, has been observed.

The gross conversion CB is taken as equal to: CB =% wt. Of 380 ° C less than the effluent, with "380 ° C minus" representing the fraction, distilled at a temperature of less than or equal to 380 ° C. The yield of middle distillates (150-380 ° C.) is equal to the weight of compounds having a boiling point of between 150 and 380 ° C. in the effluents.

The reaction temperature is set so as to reach a gross conversion CB equal to 70% by weight.

Table 6: Catalytic Activities of Hydrocracking Catalysts.

Rdt Naphta Rdt kerosene Rdt Gasole Rdt Distillais Means

Catalyst T (° C)

(% wt) (% wt) (% wt) (% wt)

1A 378 17 24.6 21, 3 45.9

1B 376 15.5 25.4 22.5 47.9

2A 370 17.1 25.0 21, 1 46.1

2B 368 15.8 25.2 22.5 47.7

3A 366 17.8 25.1 20.3 45.4

3B 364 16.2 25.3 21.5 46.8

The catalysts according to the invention (1B, 2B and 3B) clearly show higher catalytic performances than non-compliant catalysts (1A, 2A and 3A).

Catalyst 1 B shows a gain of 2.0% by weight of middle distillates in comparison with catalyst 1A and a gain in activity of 2 ° C. Catalyst 2B is more selective at 1.6% by weight and more active at 2 ° C than catalyst 2A. Catalyst 3B has an improved middle distillate yield of 1.4% by weight with a 2 ° C reaction temperature gain compared to non-conforming catalyst 3A.

The amount of naphtha produced is significantly reduced by the use of the catalyst according to the invention. Thanks to the implementation of the invention, a gain in selectivity of middle distillates is obtained without loss of activity.

These increases in selectivity are very important at the level of the refining margins: a gain of 2 ° C represents 1 to 3 months of additional industrial cycle (hence a productivity gain) and a gain of 2 points of selectivity represents an increased production 1-3% in middle distillates (gain in quantity of high added value products).

Claims

1 -Catalyst containing a support comprising at least one binder and at least one zeolite having at least one series of channels whose opening is defined by a ring containing 12 oxygen atoms, said catalyst comprising phosphorus, at least one succinate of C1-C4 dialkyl, acetic acid and a hydro-dehydrogenating functional group comprising at least one group VIB element and at least one group VIII element, whose Raman spectrum comprises the 990 and / or 974 cm ^-1 bands characteristics of at least one Keggin heteropolyanion, the characteristic bands of said succinate and the 896 cm ^-1 main band characteristic of acetic acid. 2-A catalyst according to claim 1 wherein the dialkyl succinate is dimethyl succinate and in which the catalyst has in its spectrum the main Raman bands at 990 and / or 974 cm ^-1 characteristic of Keggin heteropolyanions, and 853 cm ^-1 characteristic of the succinate d dimethyl and 896 cm ^-1 characteristic of acetic acid. 3-Catalyst according to claim 1 wherein the dialkyl succinate is diethyl succinate, dibutyl succinate or diisopropyl succinate.

4. Catalyst according to one of the preceding claims comprising a support consisting of alumina and zeolite.

5. Catalyst according to one of the preceding claims comprising a support consisting of silica-alumina and zeolite.

6. Catalyst according to one of the preceding claims also comprising boron and / or fluorine.

7. Catalyst according to one of the preceding claims wherein the zeolite is selected from the group consisting of zeolites FAU, BEA, ISV, IWR, IWW, MEI, UWY. 8. Catalyst according to claim 7 wherein the zeolite is selected from zeolite Y and / or zeolite beta. 9- Catalyst according to one of the preceding claims and sulfide.

10- Process for preparing a catalyst according to one of the preceding claims, said method comprising the following successive steps: a) at least one step of impregnating a support, comprising at least one binder and at least one zeolite having at least one series of channels whose opening is defined by a ring containing 12 oxygen atoms, by at least one solution containing the elements of the hydro-dehydrogenating function, and phosphorus b) drying at a temperature below 180 ° C without subsequent calcination c) at least one impregnation step with an impregnating solution comprising at least one C1-C4 dialkyl succinate, acetic acid and at least one phosphorus compound, if it does not was introduced in step a) d) a step of maturing, e) a drying step at a temperature below 180 ° C, without subsequent calcination step.

11 - Process according to claim 10 wherein the totality of the hydro-dehydrogenating function is introduced during step a).

12- Method according to one of claims 10 to 11 wherein the dialkyl succinate and acetic acid are introduced into the impregnating solution of step c) in an amount corresponding to a molar ratio of dialkyl succinate by element (s) of group VIB impregnated with the catalytic precursor of between 0.15 and 2.5 mol / mol, and with a molar ratio of acetic acid per element (s) of group VIB impregnated with the catalyst precursor between 0.1 and 10 mole / mole.

13- Method according to one of claims 10 to 12, said method comprising the following successive steps: a) at least one step of dry impregnation of said support with a solution containing all the elements of the hydro-dehydrogenating function, and phosphorus, b) drying at a temperature between 75 and 130 ° C without subsequent calcination, c ) at least one step of dry impregnation with an impregnating solution comprising dimethyl succinate and acetic acid, d) a maturation step at 17-50 ° C, e) a drying step at a temperature of between 80 and 160 ° C, without subsequent calcination step.

14- Method according to one of claims 10 to 13 wherein the amount of phosphorus introduced into the catalyst, expressed in amount of oxide, is between 0.1 to 20%, preferably between 0.1 and 15% and even more preferably between 0.1 and 10% by weight. 5- Method according to one of claims 10 to 14 wherein the product obtained at the end of step e) undergoes a sulphurization step. 16-Process for hydroconversion of hydrocarbon feeds in the presence of a catalyst according to one of claims 1 to 9 or prepared by the method according to one of claims 10 to 15.